"""
双流体模型的封闭关系式

该模块实现了双流体模型所需的各种封闭关系式：
1. 对流传热系数计算
2. 相变质量流量计算
3. 湍流混合和空泡漂移
4. 壁面阻力和界面阻力
"""

import numpy as np
from typing import Dict, Tuple, Optional
from dataclasses import dataclass
from enum import Enum
import logging

# 配置日志记录
logging.basicConfig(
    level=logging.INFO,
    format='%(asctime)s - %(name)s - %(levelname)s - %(message)s'
)
logger = logging.getLogger(__name__)

class BoilingRegime(Enum):
    """沸腾状态枚举"""
    SINGLE_PHASE_LIQUID = 1  # 单相液态
    SUBCOOLED_BOILING = 2    # 过冷核态沸腾
    SATURATED_BOILING = 3    # 饱和核态沸腾
    SINGLE_PHASE_VAPOR = 4   # 单相气态

class ClosureRelations:
    """封闭关系式的实现类"""
    
    def __init__(self, geometry: Dict):
        """
        初始化封闭关系式
        
        参数:
            geometry: 几何参数字典
        """
        self.geometry = geometry
        
        # 初始化物性参数
        self.Re_l = 0.0  # 液相雷诺数
        self.Re_g = 0.0  # 气相雷诺数
        self.Pr_l = 0.0  # 液相普朗特数
        self.Pr_g = 0.0  # 气相普朗特数
        self.mu_l = 0.0  # 液相粘度
        self.mu_g = 0.0  # 气相粘度
        self.rho_l = 0.0  # 液相密度
        self.rho_g = 0.0  # 气相密度
        self.quality = 0.0  # 干度
        self.conductivity = 0.0  # 导热系数
        self.hydraulic_diameter = geometry.get('hydraulic_diameter', 0.01)  # 水力直径
        
        logger.info("初始化ClosureRelations完成，水力直径: %.4f m", self.hydraulic_diameter)
        
    def update_properties(self, fluid_props: Dict):
        """
        更新流体物性参数
        
        参数:
            fluid_props: 包含流体物性的字典
        """
        logger.debug("开始更新流体物性参数")
        
        # 更新物性参数
        self.Re_l = fluid_props.get('Re_l', 0.0)
        self.Re_g = fluid_props.get('Re_g', 0.0)
        self.Pr_l = fluid_props.get('Pr_l', 0.0)
        self.Pr_g = fluid_props.get('Pr_g', 0.0)
        self.mu_l = fluid_props.get('mu_l', 0.0)
        self.mu_g = fluid_props.get('mu_g', 0.0)
        self.rho_l = fluid_props.get('rho_l', 0.0)
        self.rho_g = fluid_props.get('rho_g', 0.0)
        self.quality = fluid_props.get('quality', 0.0)
        self.conductivity = fluid_props.get('conductivity', 0.0)
        
        # 验证参数
        self._validate_parameters()
        
        logger.debug("流体物性参数更新完成")
        
    def _validate_parameters(self):
        """验证参数的有效性"""
        try:
            assert self.Re_l >= 0, "液相雷诺数必须非负"
            assert self.Re_g >= 0, "气相雷诺数必须非负"
            assert self.Pr_l > 0, "液相普朗特数必须为正"
            assert self.Pr_g > 0, "气相普朗特数必须为正"
            assert self.mu_l > 0, "液相粘度必须为正"
            assert self.mu_g > 0, "气相粘度必须为正"
            assert self.rho_l > 0, "液相密度必须为正"
            assert self.rho_g > 0, "气相密度必须为正"
            assert 0 <= self.quality <= 1, "干度必须在0到1之间"
            assert self.conductivity > 0, "导热系数必须为正"
            assert self.hydraulic_diameter > 0, "水力直径必须为正"
        except AssertionError as e:
            logger.error("参数验证失败: %s", str(e))
            raise
            
        logger.debug("参数验证通过")
        
    def heat_transfer_coefficient(self, phase: str, pressure: float, 
                                  temp_wall: float, temp_fluid: float,
                                  temp_sat: float) -> float:
        """
        计算传热系数
        
        参数:
            phase: 相态 ('liquid' 或 'vapor')
            pressure: 压力 (Pa)
            temp_wall: 壁面温度 (K)
            temp_fluid: 流体温度 (K)
            temp_sat: 饱和温度 (K)
            
        返回:
            传热系数 (W/m²·K)
        """
        logger.info("计算传热系数: phase=%s, pressure=%.2f Pa, temp_wall=%.2f K, temp_fluid=%.2f K, temp_sat=%.2f K",
                   phase, pressure, temp_wall, temp_fluid, temp_sat)
                   
        # 确定沸腾状态
        if phase == 'liquid':
            if temp_fluid < temp_sat:  # 单相液态
                regime = BoilingRegime.SINGLE_PHASE_LIQUID
            elif temp_wall > temp_sat:  # 饱和核态沸腾
                regime = BoilingRegime.SATURATED_BOILING
            else:  # 过冷核态沸腾
                regime = BoilingRegime.SUBCOOLED_BOILING
        else:  # vapor
            regime = BoilingRegime.SINGLE_PHASE_VAPOR
            
        logger.debug("确定沸腾状态: %s", regime.name)
            
        # 根据沸腾状态计算传热系数
        htc = 0.0
        if regime == BoilingRegime.SINGLE_PHASE_LIQUID:
            htc = self._single_phase_htc(phase, pressure, temp_fluid)
        elif regime == BoilingRegime.SUBCOOLED_BOILING:
            htc = self._subcooled_boiling_htc(pressure, temp_wall, temp_fluid, temp_sat)
        elif regime == BoilingRegime.SATURATED_BOILING:
            htc = self._saturated_boiling_htc(pressure, temp_wall, temp_sat)
        else:  # SINGLE_PHASE_VAPOR
            htc = self._single_phase_htc(phase, pressure, temp_fluid)
            
        logger.info("计算得到传热系数: %.2f W/m²·K", htc)
        return htc
        
    def _single_phase_htc(self, phase: str, pressure: float, temp: float) -> float:
        """计算单相传热系数（使用Dittus-Boelter关联式）"""
        logger.debug("计算单相传热系数: phase=%s, p=%.2f Pa, T=%.2f K", 
                    phase, pressure, temp)
        
        # 获取流体物性
        if phase == 'liquid':
            Re = self.Re_l
            Pr = self.Pr_l
        else:
            Re = self.Re_g
            Pr = self.Pr_g
            
        # Dittus-Boelter关联式
        if Re > 10000:  # 湍流
            Nu = 0.023 * Re**0.8 * Pr**0.4
            flow_regime = "湍流"
        elif Re > 2300:  # 过渡区
            # 使用Gnielinski关联式
            f = (0.79 * np.log(Re) - 1.64)**(-2)
            Nu = (f/8) * (Re-1000) * Pr / (1 + 12.7 * (f/8)**0.5 * (Pr**(2/3)-1))
            flow_regime = "过渡区"
        else:  # 层流
            Nu = 3.66  # 充分发展的层流
            flow_regime = "层流"
            
        logger.debug("流动状态: %s, Nu=%.2f", flow_regime, Nu)
            
        # 计算传热系数
        k = self.conductivity  # 导热系数
        D = self.hydraulic_diameter
        htc = Nu * k / D
        
        logger.debug("计算得到单相传热系数: %.2f W/m²·K", htc)
        return htc
        
    def _subcooled_boiling_htc(self, pressure: float, temp_wall: float,
                              temp_fluid: float, temp_sat: float) -> float:
        """计算过冷核态沸腾传热系数"""
        logger.debug("计算过冷核态沸腾传热系数: p=%.2f Pa, T_w=%.2f K, T_f=%.2f K, T_sat=%.2f K",
                    pressure, temp_wall, temp_fluid, temp_sat)
        
        # 计算单相传热系数
        h_l = self._single_phase_htc('liquid', pressure, temp_fluid)
        
        # 计算核态沸腾传热系数
        h_nb = self._nucleate_boiling_htc(pressure, temp_wall, temp_sat)
        
        # 使用Chen的叠加方法
        S = self._suppression_factor(temp_wall, temp_sat)
        F = self._enhancement_factor(pressure)
        
        htc = h_l * F + h_nb * S
        
        logger.debug("Chen叠加方法: S=%.3f, F=%.3f", S, F)
        logger.debug("计算得到过冷核态沸腾传热系数: %.2f W/m²·K", htc)
        return htc
        
    def _saturated_boiling_htc(self, pressure: float, temp_wall: float,
                              temp_sat: float) -> float:
        """计算饱和核态沸腾传热系数"""
        return self._nucleate_boiling_htc(pressure, temp_wall, temp_sat)
        
    def _nucleate_boiling_htc(self, pressure: float, temp_wall: float,
                             temp_sat: float) -> float:
        """计算核态沸腾传热系数（使用简化的Rohsenow关联式）"""
        # 基本物性参数
        h_fg = 2257e3
        sigma = 0.059
        rho_l = 958
        rho_g = 0.598
        mu_l = 2.82e-4
        cp_l = 4216
        g = 9.81
        C_sf = 0.013
        
        # 温度差
        delta_T = temp_wall - temp_sat
        
        # 分步计算
        A = sigma * g * (rho_l - rho_g)
        A_sqrt = A**0.5
        
        B = mu_l * h_fg
        B_div_A = B / A_sqrt
        
        C = cp_l * delta_T
        D = C_sf * h_fg * self.Pr_l
        C_div_D = C / D
        C_div_D_pow = C_div_D**0.33
        
        # 最终计算
        q = B_div_A * C_div_D_pow
        
        return q / delta_T
        
    def _suppression_factor(self, temp_wall: float, temp_sat: float) -> float:
        """计算抑制因子"""
        delta_T = temp_wall - temp_sat
        return 1 / (1 + 2.53e-6 * self.Re_l**1.17)
        
    def _enhancement_factor(self, pressure: float) -> float:
        """计算增强因子"""
        X_tt = self._martinelli_parameter(pressure)
        if X_tt <= 0.1:
            return 1.0
        else:
            return 2.35 * (0.213 + 1/X_tt)**0.736
            
    def _martinelli_parameter(self, pressure: float) -> float:
        """计算Martinelli参数"""
        # 获取物性参数
        mu_l = self.mu_l
        mu_g = self.mu_g
        rho_l = self.rho_l
        rho_g = self.rho_g
        x = self.quality
        
        return ((1-x)/x)**0.9 * (rho_g/rho_l)**0.5 * (mu_l/mu_g)**0.1
        
    def phase_change_mass_flux(self, pressure: float, temp_l: float, 
                               temp_v: float, h_l: float, h_v: float,
                               cp_l: float, cp_v: float) -> float:
        """
        计算相变质量流量
        """
        logger.info("计算相变质量流量: p=%.2f Pa, T_l=%.2f K, T_v=%.2f K", 
                   pressure, temp_l, temp_v)
        
        # 获取饱和状态参数
        h_l_sat = self._get_saturation_enthalpy(pressure, 'liquid')
        h_v_sat = self._get_saturation_enthalpy(pressure, 'vapor')
        r = h_v_sat - h_l_sat  # 汽化潜热
        
        logger.debug("饱和参数: h_l_sat=%.2f J/kg, h_v_sat=%.2f J/kg, r=%.2f J/kg",
                    h_l_sat, h_v_sat, r)
        
        # 计算各种状态下的相变质量流量
        gamma_l_sh = self._superheated_liquid_mass_flux(h_l, h_l_sat, r, cp_l)
        gamma_v_sh = self._superheated_vapor_mass_flux(h_v, h_v_sat, r, cp_v)
        gamma_l_sc = self._subcooled_liquid_mass_flux(h_l, h_l_sat, r, cp_l)
        gamma_v_sc = self._subcooled_vapor_mass_flux(h_v, h_v_sat, r, cp_v)
        
        # 计算净相变质量流量
        gamma_net = (gamma_l_sh + gamma_v_sh) - (gamma_l_sc + gamma_v_sc)
        
        logger.info("计算得到净相变质量流量: %.2f kg/m²·s", gamma_net)
        return gamma_net
        
    def turbulent_mixing_void_drift(self, gap_width: float, 
                                    mixing_length: float,
                                    rho_l: float, rho_v: float,
                                    alpha_ij: float, alpha_ii: float) -> float:
        """
        计算湍流混合和空泡漂移质量流量
        
        参数:
            gap_width: 间隙宽度 (m)
            mixing_length: 混合长度 (m)
            rho_l: 液相密度 (kg/m³)
            rho_v: 气相密度 (kg/m³)
            alpha_ij: 相邻子通道的空泡分数
            alpha_ii: 当前子通道的空泡分数
            
        返回:
            湍流混合和空泡漂移质量流量 (kg/m²·s)
        """
        # 计算涡扩散率
        C_e = 0.02  # 典型值
        
        # 计算平衡空泡分布
        alpha_equil = self._calculate_equilibrium_void_distribution(
            alpha_ij, alpha_ii, rho_l, rho_v)
            
        # 计算湍流混合和空泡漂移质量流量
        return (C_e * (gap_width/mixing_length) * (rho_l - rho_v) *
                (alpha_ij - alpha_ii - (alpha_ij - alpha_ii - alpha_equil)))
                
    def wall_interface_friction(self, phase: str, velocity: float,
                                hydraulic_diameter: float, density: float,
                                viscosity: float, quality: float,
                                relative_roughness: float) -> Tuple[float, float]:
        """
        计算壁面阻力和界面阻力
        """
        logger.info("计算壁面和界面阻力: phase=%s, v=%.2f m/s, quality=%.3f",
                   phase, velocity, quality)
        
        # 计算雷诺数
        reynolds = density * velocity * hydraulic_diameter / viscosity
        logger.debug("雷诺数: %.2f", reynolds)
        
        # 计算摩擦因子
        if reynolds < 2300:  # 层流
            f = 64 / reynolds
            flow_regime = "层流"
        elif reynolds > 4000:  # 湍流
            A = -2 * np.log10(relative_roughness/3.7 + 2.51/reynolds)
            f = 1 / A**2
            flow_regime = "湍流"
        else:  # 过渡区
            f_lam = 64 / 2300
            A = -2 * np.log10(relative_roughness/3.7 + 2.51/4000)
            f_turb = 1 / A**2
            f = f_lam + (f_turb - f_lam) * (reynolds - 2300) / 1700
            flow_regime = "过渡区"
            
        logger.debug("流动状态: %s, 摩擦因子: %.4f", flow_regime, f)
        
        # 计算壁面阻力系数
        tau_w = f * density * velocity**2 / 8
        
        # 计算界面阻力系数
        if phase == 'liquid':
            c = 20  # Chisholm系数
            density_vapor = self.rho_g
            X2 = (1-quality)**2 / quality**2 * (density/density_vapor)
            phi_l2 = 1 + c/np.sqrt(X2) + 1/X2
            tau_i = tau_w * phi_l2
            logger.debug("Chisholm系数: %.2f, 两相流系数: %.2f", c, phi_l2)
        else:
            tau_i = 0
            
        logger.info("计算得到: 壁面阻力=%.2f N/m², 界面阻力=%.2f N/m²", tau_w, tau_i)
        return tau_w, tau_i
        
    def _calculate_condensation_factor(self, pressure: float, 
                                      temp_wall: float,
                                      temp_sat: float) -> float:
        """计算冷凝因子"""
        # 简化模型，根据过热度计算
        delta_t = temp_wall - temp_sat
        return np.exp(-0.1 * delta_t)  # 示例关系式
        
    def _get_saturation_enthalpy(self, pressure: float, 
                                 phase: str) -> float:
        """获取饱和焓值"""
        # 需要实现查表或其他方法获取饱和焓值
        pass
        
    def _calculate_equilibrium_void_distribution(self, 
                                                 alpha_ij: float,
                                                 alpha_ii: float,
                                                 rho_l: float,
                                                 rho_v: float) -> float:
        """计算平衡空泡分布"""
        # 简化模型，假设平衡分布是密度加权平均
        return (alpha_ij * rho_v + alpha_ii * rho_l) / (rho_l + rho_v)
        
    def _superheated_liquid_mass_flux(self, h: float, h_sat: float,
                                     r: float, cp: float) -> float:
        """计算过热液相质量流量"""
        if h > h_sat:
            C_sh = 0.1  # 过热相变系数
            return C_sh * abs(h - h_sat) / (r * cp)
        return 0
        
    def _superheated_vapor_mass_flux(self, h: float, h_sat: float,
                                    r: float, cp: float) -> float:
        """计算过热气相质量流量"""
        if h > h_sat:
            C_sh = 0.1  # 过热相变系数
            return C_sh * abs(h - h_sat) / (r * cp)
        return 0
        
    def _subcooled_liquid_mass_flux(self, h: float, h_sat: float,
                                    r: float, cp: float) -> float:
        """计算过冷液相质量流量"""
        if h < h_sat:
            C_sc = 0.1  # 过冷相变系数
            return C_sc * abs(h - h_sat) / (r * cp)
        return 0
        
    def _subcooled_vapor_mass_flux(self, h: float, h_sat: float,
                                   r: float, cp: float) -> float:
        """计算过冷气相质量流量"""
        if h < h_sat:
            C_sc = 0.1  # 过冷相变系数
            return C_sc * abs(h - h_sat) / (r * cp)
        return 0
        
    def interface_shear(self, u_l: float, u_g: float, alpha_l: float,
                        rho_l: float, rho_g: float) -> float:
        """
        计算界面剪切力
        """
        logger.info("计算界面剪切力: u_l=%.2f m/s, u_g=%.2f m/s, alpha_l=%.3f",
                   u_l, u_g, alpha_l)
        
        # 计算界面阻力系数
        c_lv = self._get_interface_drag_coefficient(alpha_l, rho_l, rho_g)
        
        # 计算相对速度
        u_rel = abs(u_g - u_l)
        
        # 计算界面面积密度
        alpha_g = 1.0 - alpha_l
        if alpha_g < 0.3:
            flow_pattern = "气泡流"
            a_lv = 6.0 * alpha_g / self.config['bubble_diameter']
        elif alpha_g > 0.7:
            flow_pattern = "液滴流"
            a_lv = 6.0 * alpha_l / self.config['droplet_diameter']
        else:
            flow_pattern = "环状流"
            a_lv = 4.0 / self.config['hydraulic_diameter']
            
        logger.debug("流型: %s, 界面面积密度: %.2f m²/m³", flow_pattern, a_lv)
        
        # 计算界面剪切力
        tau_i = 0.5 * c_lv * rho_l * u_rel**2 * a_lv
        
        logger.info("计算得到界面剪切力: %.2f N/m²", tau_i)
        return tau_i
        
    def _get_interface_drag_coefficient(self, alpha_l: float, 
                                        rho_l: float, rho_g: float) -> float:
        """计算界面阻力系数"""
        logger.debug("计算界面阻力系数: alpha_l=%.3f", alpha_l)
        
        alpha_g = 1.0 - alpha_l
        
        # 根据流型确定阻力系数
        if alpha_g < 0.3:  # 气泡流
            # 使用气泡流的阻力系数模型
            c_d = 24.0 / self.config['bubble_reynolds']  # Stokes law
            if self.config['bubble_reynolds'] > 1.0:
                c_d = 24.0 / self.config['bubble_reynolds'] * (1.0 + 0.15 * 
                      self.config['bubble_reynolds']**0.687)  # Schiller-Naumann
            
            c_lv = 0.75 * c_d * alpha_g * rho_l / self.config['bubble_diameter']
            flow_pattern = "气泡流"
            
        elif alpha_g > 0.7:  # 液滴流
            # 使用液滴流的阻力系数模型
            c_d = 24.0 / self.config['droplet_reynolds']  # Stokes law
            if self.config['droplet_reynolds'] > 1.0:
                c_d = 24.0 / self.config['droplet_reynolds'] * (1.0 + 0.15 * 
                      self.config['droplet_reynolds']**0.687)  # Schiller-Naumann
                      
            c_lv = 0.75 * c_d * alpha_l * rho_g / self.config['droplet_diameter']
            flow_pattern = "液滴流"
            
        else:  # 环状流
            # 使用环状流的阻力系数模型
            c_lv = 0.005 * (1.0 + 75.0 * (1.0 - alpha_g))
            c_lv *= (rho_l / rho_g)**0.5
            flow_pattern = "环状流"
            
        logger.debug("流型: %s, 界面阻力系数: %.4f", flow_pattern, c_lv)
        return c_lv 